CN103382145A - Preparation process for propylene from methanol or dimethyl ether - Google Patents
Preparation process for propylene from methanol or dimethyl ether Download PDFInfo
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- CN103382145A CN103382145A CN2012101362585A CN201210136258A CN103382145A CN 103382145 A CN103382145 A CN 103382145A CN 2012101362585 A CN2012101362585 A CN 2012101362585A CN 201210136258 A CN201210136258 A CN 201210136258A CN 103382145 A CN103382145 A CN 103382145A
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Abstract
The invention relates to a preparation process for propylene from methanol or dimethyl ether. The process comprises the following steps: allowing the raw materials consisting of methanol or dimethyl ether, water and above-C4 components returned from a separation system to undergo a reaction in a first reactor so as to produce propylene-rich C1-C10 components which enter into the separation system; separating propylene from the separation system as a product and allowing above-C4 components to return to the reactor; and subjecting C1-C2 components in the separation system to a reaction in a second reactor to produce above-C3 high-carbon substances and returning the above-C3 high-carbon substances to the separation system to promote yield of propylene; wherein selectivity of propylene in the first reactor is greater than 70%, and the yield of propylene after propylene-yield promotion by the second reactor is greater than 75%. Compared with the prior art, the process provided by the invention has the advantages of high selectivity of the product propylene, no need for an ethylene cryogenic fractionation system, low content of C2 and below-C2 components, simplification of the separation system and substantial reduction of energy consumption of the separation system.
Description
Technical field
The present invention relates to the technique of a kind of methyl alcohol or dme propylene processed.
Background technology
Propylene is a kind of important Organic Chemicals, mainly for the production of polypropylene, vinyl cyanide and vinylformic acid.Propylene is mainly obtained through steam cracking or catalytic cracking by petroleum at present, and its price is affected by oil price.It is essential that the production of propylene technique that the in short supply and growing propylene market requirement of petroleum resources reserves makes exploitation not rely on oil becomes.So simultaneously, domestic methyl alcohol production capacity is seriously superfluous, and methanol prices is cheap.Exploitation preparing propylene from methanol (MTP) technology can be utilized reserves abundant coal or natural gas via preparing propylene from methanol, opens up a Non oil-based route production of propylene technology, has wide market outlook and realistic meaning.
At present, industrialized preparing propylene from methanol (MTP) technology adopts multistage insulation formula fixed-bed reactor (WO2006/136433A1, WO2007/140844A1), adopt the ZSM-5 catalyzer of modification, main reactor divides six layers, intersegmental cold shock feed control temperature, the ethylene component in separation system except propylene product, carbon four loop back reactor to improve the yield (WO2007/04212A1) of propylene to carbon six components.This technological process reactor temperature control system is complicated, and inconvenience is controlled in operation.Propylene Selectivity is 65%, and propene yield is on the low side, and unit consumption of product is high.And, there is a large amount of ethene (account for propone output 38%) step of Returning reactor after the separation system deep cooling in this technological process, boiling point very low (under normal pressure being-102 ℃) due to ethene, in system, the partitioning cycle of a large amount of ethene causes the separation system compressors energy consumption high, and the low temperature separation process cost is high.
Chinese patent CN 101177374A discloses a kind of ethene and the methyl alcohol coreaction improves the methyl alcohol of Propylene Selectivity or the method that dme generates propylene.The method reacts ethylene product and the methyl alcohol that process produces, and comes propylene enhancing.Patent CN 101747133A discloses and a kind of ethene in the methanol-to-olefins product and butylene are carried out anti-disproportionation reaction and generate propylene being different from the methanol to olefins reaction catalyzer.
Chinese patent CN 101629090A discloses the technique that a kind of methyl alcohol generates the hydrocarbon products that is rich in propylene, and the characteristics of this technique are not exist alkene to loop back the process of reactor, but the higher olefins in the methanol-to-olefins product is processed into gasoline.Patent CN 102351629A also discloses the patent of preparing propylene from methanol by-product gasoline, is characterised in that and passes through C
4Material and methyl alcohol generation etherification reaction and C
2Material generation building-up reactions generates blend gasoline.
Chinese patent CN 101830769A discloses a kind of process for preparing propylene from methanol, it is characterized in that this technological process is with the C in the preparing propylene from methanol separation system
2And C
4Component enters the first reaction zone, C
5～C
7Component enters second reaction zone, respectively at different reactor area and methyl alcohol coreaction.Patent CN 101417914A discloses a kind of methyl alcohol and C
4Above hydro carbons is the process of waste propylene.This technological process adds the higher hydrocarbons cracking in the MTP system, can reduce the heat effect of MTP.But the reactive system raw material is not single methyl alcohol.
The ethylene separation circulation that existing MTP industrialized unit exists causes the problem that the sepn process cost is high, energy consumption is high.
Summary of the invention
Purpose of the present invention be exactly provide in order to overcome the defective that above-mentioned prior art exists that a kind of Propylene Selectivity is high, the technique of the simple methyl alcohol of technique or dme propylene processed.
Purpose of the present invention can be achieved through the following technical solutions: the technique of a kind of methyl alcohol or dme propylene processed, it is characterized in that, and this technique comprises the following steps:
(1) C that raw material, water and separation system is returned
4After above component was mixed, in input the first reactor, reaction generated the C that is rich in propylene
1-C
10Hydrocarbon component and water;
(2) step (1) products therefrom enters the separation system separation, and aqueous portion returns in the first reactor, and gas phase is the organic hydrocarbon component, enters primary fractionation system, isolates successively C in primary fractionation system
1-C
2Component, C
3Component and C
4-C
10Component, wherein C
4-C
10Component enters takes off rectifying in the gasoline tower, and the isolated component of tower top is returned to the first reactor and continued reaction, described C
3Component is directly as product or enter propylene tower and separate and to obtain propylene and propane;
(3) described C
1-C
2Component directly enters the second reactor after heating, it is C that reaction generates main ingredient
3Above high-carbon thing, the second reactor reaction product enters gas-liquid separator after cooling, and act as a fuel gas and part of gas phase returned to the second reactor, and liquid phase is returned to primary fractionation system.
The described raw material of step (1) is methyl alcohol or dme, perhaps is the mixture of methyl alcohol, dme and the water of methyl alcohol after the pre-reactor Partial Conversion is dme.
The mass ratio of the described water of step (1) and raw material is 0-10: 1, and the C that described separation system is returned
4Above component and the mass ratio of raw material are 0.2-10: 1, and raw material is with CH
2Meter.
The mass ratio of the described water of step (1) and raw material is 0.2-7: 1, and the C that described separation system is returned
4Above component and the mass ratio of raw material are 1-3: 1, and raw material is with CH
2Meter.
The temperature of reaction of described the first reactor is 380-550 ℃, and reaction pressure is 0.1～0.3MPa, and the charging weight hourly space velocity of raw material is 1～10h
-1, the transformation efficiency of raw material is 90～100%; The employing ZSM-5 molecular sieve catalyzer of described the first reactor or through the ZSM-5 molecular sieve of modification, the sial of molecular sieve (Si/Al) is than being 50～500;
Described the first reactor is fixed-bed reactor, a kind of in fluidized-bed reactor or moving-burden bed reactor;
When adopting fixed-bed reactor, the first reactor is made of one or more fixed-bed reactor parallel connection, and fixed-bed reactor are calandria type fixed bed reactor, and catalyst loading is in tubulation or between tubulation; Be perhaps multistage insulation formula reactor, middle cold shock charging or indirect heat exchange;
The temperature of reaction of described the first reactor is 430-500 ℃, reaction pressure 0.1～0.2MPa, and the charging weight hourly space velocity of raw material is 2-5h
-1
Described the first reactor is made of the parallel connection of 2-5 platform fixed-bed reactor.
Described the second reactor adopts solid phosphoric acid catalyst or ZSM-5 molecular sieve catalyzer, and 200～500 ℃ of temperature of reaction, reaction pressure are 0.2-2MPa, and charging volume of ethylene concentration is 10%～100%, and ethene mark attitude air speed is 1000h
-1～7000h
-1Described ZSM-5 molecular sieve catalyzer sial (Si/Al) is than being 10～500;
Described the second reactor is a kind of in insulation fix bed reactor, calandria type fixed bed reactor or fluidized-bed reactor.When adopting the fixed bed pattern, the second reactor is made of one or many reactor parallel connections.
Described ZSM-5 molecular sieve catalyzer sial (Si/Al) is than being 10～200;
Described the second reactor is made of the parallel connection of 2-5 platform reactor when adopting the fixed bed pattern.
The second reactor reaction product enters gas-liquid separator after cooling, the cooled temperature of reaction product gas is-20 ℃～50 ℃.In gas-liquid separator, gas-phase product as fuel gas product, returns to the second reactor but also can partly circulate, and liquid phase circulation returns to primary fractionation system, but also can return to the first reactor.Described primary fractionation system comprises deethanizing column, depropanizing tower, and the part or all of combination of debutanizing tower, the logistics that enters primary fractionation system is introduced into deethanizing column, or is introduced into depropanizing tower, perhaps is introduced into debutanizing tower.
The ethylene separation circulation that the present invention is directed to existing MTP industrialized unit existence causes the problem that the sepn process cost is high, energy consumption is high, the invention provides a kind of technological process of saving the step of a large amount of ethene compression partitioning cycle and improving Propylene Selectivity.Be in reaction process, the C that adopts methyl alcohol and separation system to produce
4Above component coreaction obtains P/E than the high propylene product that is rich in; In product, propylene is as product; C
1-C
2Component changes into higher hydrocarbons by the second reactor, returns to separation system; C
4Above component is through removing C
7Return to the first reactor after above component to improve Propylene Selectivity.In the first reactor, Propylene Selectivity is greater than 70%, and system's propene yield is greater than 75% after the second reactor propylene enhancing.This technological process product Propylene Selectivity is high, need not ethene deep cooling fractionating system and C
2And following component concentration is low, has simplified separation system and has significantly reduced the separation system energy consumption.
Compared with prior art, the invention has the beneficial effects as follows:
1, reactive system process methyl alcohol and C
4Above component coreaction by rational proportion, generates product and has higher propylene and ethylene ratio, has avoided a large amount of generations of ethene.Make the yield of propylene improve.
2, few owing to generating the ethene amount, product gas compression and separating energy consumption significantly reduce, and separation process shortens.
3, adopt C
1-C
2Hydrocarbon conversion process makes part ethene generate high-carbon hydrocarbon, after Returning reacting system, has further improved the yield of propylene.
The overall selectivity of the final propylene of this process is greater than 75%, and without ethylene separation circulating reaction step, separating energy consumption significantly reduces.
Description of drawings
Fig. 1 is reacting flow chart of the present invention.
In figure: 1 for storage tank, 2 for pre-reactor, 3 be the first reactor, 4 for separator, 5 for primary fractionation system, 6 be that the second reactor, 7 is C for separator bottoms stream, 15 for top exit logistics, 14 that to take off gasoline tower, 9 be component, the 13-separator of the first reactor outlet for feed stream, 11 for mixture flow, 12 for propylene tower, 10 for gas-liquid separator, 8
4-C
10Component, 16 is C
1-C
2Component, 17 is C
3Component, 18 is that the second reactor reaction product, 19 gas phase, 20 liquid phases, 21 that go out for gas-liquid separator separates that go out for gas-liquid separator separates are gasoline component, and 22 is that propylene, 24 is propane for taking off gasoline tower bottom product, 23.
Embodiment
The present invention is described in detail below in conjunction with the drawings and specific embodiments.
Reaction process of the present invention as shown in Figure 1,
(1) material benzenemethanol is exported from storage tank 1, feed stream 10 enters pre-reactor 2, and before entering pre-reactor 2, logistics is heated to 200-300 ℃.Methyl alcohol part in pre-reactor 2 changes into dme.The product of pre-reactor 2 is first with from C at the bottom of the tower of separator 4
4After above component is mixed, then and come the 8 isolated logistics 21 of tower top of autospasy gasoline tower to mix, mixture flow 11 enters the first reactor 3, in the first reactor 3, methyl alcohol or dimethyl ether conversion are the alkene that is rich in propylene, transformation efficiency is 90%～100%.The temperature 380-550 of the first reactor 3 ℃, pressure is 0.1-2MPa.
(2) component 12 of step (1) products therefrom the first reactor 3 outlets enters separator 4 after cooling heat transferring, separate in separator 4, the water component is partly returned in the first reactor, another part separator bottoms stream 14 is discharged, the main hydrocarbon-containifirst of top exit logistics 13 of separator 4, these hydro carbons enter primary fractionation system 5, isolate successively C in primary fractionation system 5
1-C
2Component 16, C
3Component 17 and C
4-C
10Component 15, wherein C
4-C
10Component 15 enters takes off rectifying in gasoline tower 8, and the isolated logistics 21 of tower top is returned to the first reactor 3 and continued reaction, takes off gasoline tower bottom product 22 and discharges, described C
3Component 17 is directly as product or enter propylene tower 9 and separate and obtain propylene 23 and propane 24;
(3) described C
1-C
2Component 16 directly enters the second reactor 6 after heating, it is C that reaction generates main ingredient
3Above high-carbon thing, the second reactor reaction product 18 enters gas-liquid separator 7 after cooling, the gas phase 19 that gas-liquid separator separates the goes out gas product that acts as a fuel, the liquid phase 20 that gas-liquid separator separates goes out is returned to primary fractionation system 5.
Embodiment 1
The first reactor is comprised of two insulation fix bed reactors reaction regeneration that switches in parallel, and in every insulation fix bed reactor, take high silica ZSM-5 as catalyzer, catalyst S i/Al ratio is 50, specific surface area 350m
2/ g, pore volume 0.112ml/g.In insulation fix bed reactor, the C that methyl alcohol and separation system are returned
4Above component (is C
4Above recycle hydrocarbons) be converted into the reactant gases that is rich in propylene.The feed composition mass ratio of the first reactor: methyl alcohol is (with CH
2Meter): water: C
4Above recycle hydrocarbons=1: 10: 0.5, reaction is in methanol feeding, and the methyl alcohol weight hourly space velocity is 1h
-1, 550 ℃ of reaction-ure inlet temperature, reaction pressure 0.30MPa.The reaction result of the first reactor sees Table one.
The second reactor is comprised of two insulation fix bed reactors reaction regeneration that switches in parallel, and in every insulation fix bed reactor, take ZSM-5 as catalyzer, catalyst S i/Al ratio is 10, specific surface area 320m
2/ g, pore volume 0.102ml/g.In insulation fix bed reactor, with C
1～C
2The hydrocarbon conversion is the reactant gases that is rich in higher hydrocarbons.200 ℃ of reaction-ure inlet temperature, reaction pressure 2MPa, charging is ethene 20%+ methane 80%, ethene mark attitude air speed is 1000h
-1, the reaction result of the second reactor sees Table two.
Embodiment 2
The first reactor is composed in parallel by five insulation fix bed reactors, four reactions, and one is used for catalyst regeneration.In every insulation fix bed reactor, take high silica ZSM-5 as catalyzer, catalyst S i/Al ratio is 220, specific surface area 350m
2/ g, pore volume 0.112ml/g.In insulation fix bed reactor, with methyl alcohol and C
4Above higher hydrocarbons is converted into the reactant gases that is rich in propylene.The feed composition mass ratio of the first reactor: dme is (with CH
2Meter): water: C
4Above recycle hydrocarbons=1: 5: 4, reaction is in methanol feeding, and the methyl alcohol weight hourly space velocity is 3h
-1, 460 ℃ of reaction-ure inlet temperature, reaction pressure 0.1MPa.The reaction result of the first reactor sees Table one.
The second reactor is composed in parallel by two calandria type fixed bed reactors near isothermal, a reaction, and one is used for catalyst regeneration.In every reactor, take high silica ZSM-5 as catalyzer, catalyst S i/Al ratio is 500, specific surface area 320m
2/ g, pore volume 0.102ml/g.In the calandria type fixed bed reactor near isothermal, with C
1～C
2The hydrocarbon conversion is the reactant gases that is rich in higher hydrocarbons.350 ℃ of reaction-ure inlet temperature, reaction pressure 0.8MPa, charging is ethene 100%, ethene mark attitude air speed is 7000h
-1The reaction result of the second reactor sees Table two.
Embodiment 3
The first reactor is composed in parallel by three insulation fix bed reactors with the intermediate raw material cold shock, two reactions, a regeneration.In every insulation fix bed reactor, take high silica ZSM-5 as catalyzer, catalyst S i/Al ratio is 500, specific surface area 350m
2/ g, pore volume 0.112ml/g.In reactor, with methyl alcohol and C
4Above higher hydrocarbons is converted into the reactant gases that is rich in propylene.380 ℃ of reaction-ure inlet temperature, reaction pressure 0.13MPa, the feed composition mass ratio of the first reactor are that methyl alcohol is (with CH
2Meter): water: C
4Above recycle hydrocarbons=1: 0: 10, reaction is in methanol feeding, and air speed is 10h
-1The reaction result of the first reactor sees Table one.
The second reactor is composed in parallel by five calandria type fixed bed reactors near isothermal, and four are used for reaction, a regeneration.In every reactor, take ZSM-5 as catalyzer, catalyst S i/Al ratio is 20, specific surface area 320m
2/ g, pore volume 0.102ml/g.In the second reactor, with C
1～C
2The hydrocarbon conversion is the reactant gases that is rich in higher hydrocarbons.500 ℃ of reaction-ure inlet temperature, reaction pressure 0.2MPa, charging is ethene 10%+ methane 90%, ethene mark attitude air speed is 5000h
-1The reaction result of the second reactor sees Table two.
Embodiment 4
The first reactor is a kind of moving-burden bed reactor, and in reactor, take high silica ZSM-5 as catalyzer, catalyst S i/Al ratio is 220, specific surface area 350m
2/ g, pore volume 0.112ml/g.In reactor, with methyl alcohol and C
4Above higher hydrocarbons is converted into the reactant gases that is rich in propylene.The feed composition mass ratio of the first reactor is that methyl alcohol is (with CH
2Meter): water: C
4Above recycle hydrocarbons=1: 2: 3, reaction is in methanol feeding, and air speed is 5h
-1, 430 ℃ of reaction-ure inlet temperature, reaction pressure 0.13MPa.The reaction result of the first reactor sees Table one.
The second reactor is fluidized-bed reactor; In reactor, take the ZSM-5 of P modification as catalyzer, catalyst S i/Al ratio is 25, specific surface area 320m
2/ g, pore volume 0.102ml/g.In fluidized-bed reactor, with C
1～C
2The hydrocarbon conversion is the reactant gases that is rich in higher hydrocarbons.500 ℃ of reaction-ure inlet temperature, reaction pressure 0.2MPa, charging is ethene 90%+ methane 10%, ethene mark attitude air speed is 1000h
-1The reaction result of the second reactor sees Table two.
Described primary fractionation system comprises deethanizing column, depropanizing tower, and the part or all of combination of debutanizing tower, the logistics that enters primary fractionation system is introduced into deethanizing column, and the deethanizing tower top obtains C
1-C
2Component, at the bottom of the deethanizing column tower, component enters depropanizing tower again, and the depropanizing tower tower top obtains C
3Component, C at the bottom of tower
4Above component.
Embodiment 5
The technique of a kind of methyl alcohol or dme propylene processed, this technique comprises the following steps:
(1) C that material benzenemethanol, water and separation system is returned
4After above component was mixed, in input the first reactor, reaction generated the C that is rich in propylene
1-C
10Hydrocarbon component and water; The mass ratio of described water and raw material is 0: 1, the C that described separation system is returned
4Above component and the mass ratio of raw material are 3: 1, and raw material is with CH
2Meter;
(2) step (1) products therefrom enters the separation system separation, and aqueous portion returns in the first reactor, and gas phase is the organic hydrocarbon component, enters primary fractionation system, isolates successively C in primary fractionation system
1-C
2Component, C
3Component and C
4-C
10Component, wherein C
4-C
10Component enters takes off rectifying in the gasoline tower, and the isolated component of tower top is returned to the first reactor and continued reaction, described C
3Component is directly as product or enter propylene tower and separate and to obtain propylene and propane;
The temperature of reaction of described the first reactor is 500 ℃, and reaction pressure is 0.2MPa, and the charging weight hourly space velocity of raw material is 5h
-1, the transformation efficiency of raw material is 96.3%; The employing ZSM-5 molecular sieve catalyzer of described the first reactor, the silica alumina ratio of molecular sieve (Si/Al) is 200: 1; The first reactor is for adopting the circulating fluid bed reactor with continuous catalyst regenerating.The reaction result of the first reactor sees Table one.
(3) described C
1-C
2Component directly enters the second reactor after heating, it is C that reaction generates main ingredient
3Above high-carbon thing, the second reactor reaction product enters gas-liquid separator after cooling, and gas phase is emptying, and liquid phase is returned to primary fractionation system.
Described the second reactor adopts solid phosphoric acid catalyst, and 300 ℃ of temperature of reaction, reaction pressure are 0.5MPa, and charging volume of ethylene concentration is 60%, and ethene mark attitude air speed is 3000h
-1The second reactor is the insulation fix bed reactor with intermediate raw material charging cold shock.The reaction result of the second reactor sees Table two.
Described primary fractionation system comprises deethanizing column, depropanizing tower, and the part or all of combination of debutanizing tower, the logistics that enters primary fractionation system is introduced into depropanizing tower, and at the bottom of the depropanizing tower tower, component obtains C
4Above component, depropanizing tower tower top component enters deethanizing column again.The deethanizer overhead component is C
1-C
2Component obtains C at the bottom of tower
3Component.
Table one
Table two
Claims (10)
1. the technique of a methyl alcohol or dme propylene processed, is characterized in that, this technique comprises the following steps:
(1) C that raw material, water and separation system is returned
4After above component was mixed, in input the first reactor, reaction generated the C that is rich in propylene
1-C
10Hydrocarbon component and water;
(2) step (1) products therefrom enters the separation system separation, and aqueous portion returns in the first reactor, and gas phase is the organic hydrocarbon component, enters primary fractionation system, isolates successively C in primary fractionation system
1-C
2Component, C
3Component and C
4-C
10Component, wherein C
4-C
10Component enters takes off rectifying in the gasoline tower, and the isolated component of tower top is returned to the first reactor and continued reaction, described C
3Component is directly as product or enter propylene tower and separate and to obtain propylene and propane;
(3) described C
1-C
2Component directly enters the second reactor after heating, it is C that reaction generates main ingredient
3Above high-carbon thing, the second reactor reaction product enters gas-liquid separator after cooling, and act as a fuel gas and part of gas phase returned to the second reactor, and liquid phase is returned to primary fractionation system.
2. the technique of a kind of methyl alcohol according to claim 1 or dme propylene processed, it is characterized in that, the described raw material of step (1) is methyl alcohol or dme, perhaps is the mixture of methyl alcohol, dme and the water of methyl alcohol after the pre-reactor Partial Conversion is dme.
3. the technique of a kind of methyl alcohol according to claim 1 or dme propylene processed, it is characterized in that, the mass ratio of the described water of step (1) and raw material is 0-10: 1, and the component that the C4 that described separation system is returned is above and the mass ratio of raw material are 0.2-10: 1, raw material is with CH
2Meter.
4. the technique of a kind of methyl alcohol according to claim 3 or dme propylene processed, is characterized in that, the mass ratio of the described water of step (1) and raw material is 0.2-7: 1, and the C that described separation system is returned
4Above component and the mass ratio of raw material are 1-3: 1, and raw material is with CH
2Meter.
5. the technique of a kind of methyl alcohol according to claim 1 or dme propylene processed, is characterized in that, the temperature of reaction of described the first reactor is 380-550 ℃, and reaction pressure is 0.1～0.3MPa, and the charging weight hourly space velocity of raw material is 1～10h
-1, the transformation efficiency of raw material is 90～100%; Described the first reactor adopts the ZSM-5 molecular sieve catalyzer or through the ZSM-5 molecular sieve of modification, the silica alumina ratio of molecular sieve (Si/A1) is 50～500;
Described the first reactor is fixed-bed reactor, a kind of in fluidized-bed reactor or moving-burden bed reactor;
When adopting fixed-bed reactor, the first reactor is made of one or more fixed-bed reactor parallel connection, and fixed-bed reactor are calandria type fixed bed reactor, and catalyst loading is in tubulation or between tubulation; Be perhaps multistage insulation formula reactor, middle cold shock charging or indirect heat exchange.
6. the reactor of a kind of methyl alcohol according to claim 5 or dme propylene processed, is characterized in that, the temperature of reaction of described the first reactor is 430-500 ℃, reaction pressure 0.1～0.2MPa, and the charging weight hourly space velocity of raw material is 2-5h
-1
Described the first reactor is made of the parallel connection of 2-5 platform fixed-bed reactor.
7. the technique of a kind of methyl alcohol according to claim 1 or dme propylene processed, it is characterized in that, described the second reactor adopts solid phosphoric acid catalyst or ZSM-5 molecular sieve type catalyzer, 200～500 ℃ of temperature of reaction, reaction pressure is 0.2-2MPa, charging volume of ethylene concentration is 10%～100%, and ethene mark attitude air speed is 1000h
-1～7000h
-1Described ZSM-5 molecular sieve catalyzer sial (Si/Al) is than being 10～500;
Described the second reactor is a kind of in insulation fix bed reactor, calandria type fixed bed reactor or fluidized-bed reactor, and the second reactor is made of one or many reactor parallel connections.
8. the technique of a kind of methyl alcohol according to claim 7 or dme propylene processed, is characterized in that, described ZSM-5 molecular sieve catalyzer silica alumina ratio (Si/Al) is 10～200;
Described the second reactor is made of the parallel connection of 2-5 platform reactor.
9. the technique of a kind of methyl alcohol according to claim 1 or dme propylene processed, it is characterized in that, described the second reactor reaction product enters gas-liquid separator after cooling, the cooled temperature of reaction product gas is-20 ℃～50 ℃, the gas-phase product gas product that acts as a fuel in gas-liquid separator, perhaps the second reactor is returned in the part circulation, and liquid phase circulation returns to primary fractionation system, perhaps returns to the first reactor.
10. the technique of a kind of methyl alcohol according to claim 1 or dme propylene processed, it is characterized in that, described primary fractionation system comprises deethanizing column, depropanizing tower, the part or all of combination of debutanizing tower, the logistics that enters primary fractionation system is introduced into deethanizing column, or is introduced into depropanizing tower, perhaps is introduced into debutanizing tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210136258.5A CN103382145B (en) | 2012-05-02 | 2012-05-02 | Preparation process for propylene from methanol or dimethyl ether |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210136258.5A CN103382145B (en) | 2012-05-02 | 2012-05-02 | Preparation process for propylene from methanol or dimethyl ether |
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| Publication Number | Publication Date |
|---|---|
| CN103382145A true CN103382145A (en) | 2013-11-06 |
| CN103382145B CN103382145B (en) | 2015-06-03 |
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| CN103694072A (en) * | 2013-12-19 | 2014-04-02 | 中国石油集团东北炼化工程有限公司吉林设计院 | High-low-pressure double-tower rectification methane and ethylene removal process |
| CN106831286A (en) * | 2016-12-21 | 2017-06-13 | 江苏天诺新材料科技股份有限公司 | The method that oxide prepares low-carbon alkene |
| CN108329186A (en) * | 2017-01-18 | 2018-07-27 | 中国石油化工股份有限公司 | A kind of methanol conversion process of tandem moving bed |
| CN110577458A (en) * | 2018-06-07 | 2019-12-17 | 中国科学院大连化学物理研究所 | Method for preparing low-carbon olefin from methanol and/or dimethyl ether under high-pressure hydrogen condition |
| CN113277924A (en) * | 2021-02-04 | 2021-08-20 | 重庆文理学院 | A high-efficient heat exchange system for propylene preparation |
| CN115259982A (en) * | 2022-08-01 | 2022-11-01 | 润和催化剂股份有限公司 | Process method and reaction system for preparing propylene by methanol conversion |
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| CN103694072A (en) * | 2013-12-19 | 2014-04-02 | 中国石油集团东北炼化工程有限公司吉林设计院 | High-low-pressure double-tower rectification methane and ethylene removal process |
| CN103694072B (en) * | 2013-12-19 | 2016-04-27 | 中国石油集团东北炼化工程有限公司吉林设计院 | A kind of high-low pressure double-tower rectifying demethanizing, ethylene process |
| CN106831286A (en) * | 2016-12-21 | 2017-06-13 | 江苏天诺新材料科技股份有限公司 | The method that oxide prepares low-carbon alkene |
| CN106831286B (en) * | 2016-12-21 | 2023-08-11 | 江苏国瓷新材料科技股份有限公司 | Method for preparing low-carbon olefin by oxide |
| CN108329186A (en) * | 2017-01-18 | 2018-07-27 | 中国石油化工股份有限公司 | A kind of methanol conversion process of tandem moving bed |
| CN110577458A (en) * | 2018-06-07 | 2019-12-17 | 中国科学院大连化学物理研究所 | Method for preparing low-carbon olefin from methanol and/or dimethyl ether under high-pressure hydrogen condition |
| CN113277924A (en) * | 2021-02-04 | 2021-08-20 | 重庆文理学院 | A high-efficient heat exchange system for propylene preparation |
| CN113277924B (en) * | 2021-02-04 | 2023-05-30 | 重庆文理学院 | Heat exchange system for propylene preparation |
| CN115259982A (en) * | 2022-08-01 | 2022-11-01 | 润和催化剂股份有限公司 | Process method and reaction system for preparing propylene by methanol conversion |
| CN115259982B (en) * | 2022-08-01 | 2024-05-14 | 润和催化剂股份有限公司 | Technological method and reaction system for preparing propylene by methanol conversion |
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